KR20180004219A - Method for purifying a hydrocarbon stream using a low-reactivity adsorbent - Google Patents

Abstract

This disclosure is based on a method of removing contaminants from hydrocarbon streams, such as the removal of chlorides, CO ₂ , COS, H ₂ S, AsH ₃ , methanol, mercaptans and other S-alcohols from olefins, paraffins, aromatics, naphthenes and other hydrocarbon streams. Or O-containing organic compounds. The method involves contacting the stream with an adsorbent comprising zeolite, an alumina component and a metal component, such as sodium, in an amount of at least 30% of the ion exchange capacity of the zeolite.

Description

Method for purifying a hydrocarbon stream using a low-reactivity adsorbent

Priority statement

The present application claims priority from U.S. Provisional Application No. 62 / 222,326, filed September 23, 2015, the contents of which are incorporated herein by reference.

Field

This disclosure is based on a method of removing contaminants from hydrocarbon streams, such as the removal of chlorides, CO ₂ , COS, H ₂ S, AsH ₃ , methanol, mercaptans and other S-alcohols from olefins, paraffins, aromatics, naphthenes and other hydrocarbon streams. Or O-containing organic compounds. The method involves contacting the stream with an adsorbent comprising zeolite, a binder, and a metal component, such as sodium, in an amount of at least 30% of the ion exchange capacity of the zeolite.

Solid sorbents are commonly used to remove contaminants such as olefins, natural gas, and light hydrocarbon fractions from hydrocarbon streams. Because these streams may contain different contaminants, one or more adsorbent or adsorbent beds may be required to sufficiently purify the stream for use in the desired process. Contaminants that may be present in these streams are chloride, H ₂ O, CO, O ₂ , CO ₂ , COS, H ₂ S, NH ₃ , AsH ₃ , PH ₃ , Hg, methanol, mercaptans and other S- O-containing organic compounds.

An aromatic extraction unit which can tolerate the feed of the continuous contact reforming flat forming unit may have corrosion problems caused by chloride influx and chloride accumulation in the solvent. Current methods for removing chlorides using solid adsorbents are practiced in the art, but are costly options because of the need to process huge heavier hydrocarbon-containing streams in order to be effective.

For example, a purifier that extracts benzene from a reformed stream may apply a chloride removal phase to the benzene extraction unit on the feed. A chloride removal phase can be applied since chloride in the feed to the unit can cause corrosion issues within the unit. However, once the chloride removal phase is applied to the feed, the corrosion issue of the unit is improved as indicated by the pH control of the process stream, and more specifically, the acidic zone is greatly improved. Using this arrangement, the unit begins to have problems with benzene recovery over time. The poor recovery of benzene causes the efficiency of the solvent to be lowered by accumulating heavy oil in the solvent of the unit. The adsorbent acts as a catalyst for acid catalyzed reactions, such as alkylation of olefins with aromatic hydrocarbons. The catalytic action of the adsorbent is even enhanced when adsorbing chloride contaminants. The side reactions of the alkylation described above substantially increase the molecular weight of the feed and sometimes increase it by more than a factor of two. These high molecular weight materials accumulated in the unit are detrimental because the unit is not designed to handle such materials.

Therefore, there is a need for a method that utilizes a reasonable size and appropriately placed chloride removal phase.

A first embodiment of the present invention is a process for removing contaminants from a hydrocarbon stream comprising the steps of reacting a hydrocarbon comprising olefins, paraffins, aromatics, naphthenes, having a boiling point of from 50 DEG C to 180 DEG C, Contacting the stream with an adsorbent under adsorption conditions to remove a portion of the at least one chloride-containing contaminant, wherein the adsorbent comprises a zeolite component, a binder, and a metal component to produce a hydrocarbon product stream to be. Embodiments of the present invention are any one or any one of the preceding embodiments of the preceding embodiments in this paragraph through the first embodiment in this paragraph, wherein the zeolite is selected from the group consisting of zeolite X, zeolite Y, zeolite A, .

Embodiments of the present invention are any one or any one or all of the preceding embodiments of the preceding paragraph in the paragraph through the first embodiment in which the binder is selected from the group consisting of alumina, silica, clay, alumina silicate, titania, zirconia, And mixtures thereof. Embodiments of the present invention are any one or any one of the preceding embodiments in the preceding paragraph in this paragraph through the first embodiment in this paragraph, wherein the zeolite is zeolite X. Embodiments of the present invention are any one, any or all of the preceding embodiments of the preceding paragraph in the paragraph through the first embodiment, wherein the adsorbent has a ratio of silica to alumina of from 2.0 to 2.5, preferably 2.1 to be. Embodiments of the present invention are any one, any or all of the preceding embodiments of the preceding paragraph in the paragraph through the first embodiment in which the adsorption conditions are selected from the group consisting of a temperature of from 50 ° C to 150 ° C, . Embodiments of the present invention are any one or any one of the preceding embodiments in the preceding paragraph in the paragraph from the paragraph above to any one or all embodiments wherein the metal component is sodium, potassium, lithium, rubidium, cesium, ≪ / RTI > Embodiments of the present invention are any one, any or all of the preceding embodiments of the preceding embodiments in this paragraph through the first embodiment in this paragraph, wherein the metal component is sodium. Embodiments of the present invention are any one, any or all of the preceding embodiments of the preceding paragraph in the paragraph from the paragraph above, wherein the zeolite is present in an amount of from 30% to 95% by weight of the adsorbent .

Embodiments of the present invention are any one or any of the preceding embodiments in the preceding paragraphs in the paragraph through the first embodiment in this paragraph and wherein the step of transferring the hydrocarbon product stream to an extractive distillation unit for recovery of aromatics . The adsorbent is for removing contaminants from the hydrocarbon stream comprising the zeolite component, the binder component, and the metal component. The zeolite is selected from the group consisting of zeolite X, zeolite Y, zeolite A and mixtures thereof. The binder is selected from the group consisting of alumina, silica, clay, alumina silicate, titania, zirconia, and mixtures thereof. The adsorbent may have a silica to alumina ratio of 2.0-2.5. The metal component may be an alkali metal selected from the group consisting of sodium, potassium, lithium, rubidium, cesium, and mixtures thereof. The zeolite may be present in an amount of from 30% to 95% by weight of the adsorbent.

Additional objects, advantages and novel features of the embodiments are set forth in part in the description which follows, and in part will be obvious to those skilled in the art upon examination of the following description or may be learned by production or manipulation of embodiments. The objects and advantages of the concepts may be realized and obtained by means of the methodologies, means and combinations particularly pointed out in the appended claims.

Justice

The term "stream", "feed", "product", "portion" or "portion" as used herein refers to various hydrocarbon molecules such as linear, branched or cyclic alkanes, alkenes, alkadienes and alkynes, For example, hydrogen, or impurities such as heavy metals, and sulfur and nitrogen compounds, depending on the nature of the catalyst. Each of these may also include aromatic and non-aromatic hydrocarbons.

The hydrocarbon molecule may be abbreviated to be C ₁ , C ₂ , C ₃ , C _{n where} "n" represents the number of carbon atoms in one or more hydrocarbon molecules, or the abbreviation may be, for example, as a non-aromatic or adjective for a compound Can be used. Similarly, the aromatic compound may be abbreviated to A ₆ , A ₇ , A ₈ , A _n , where "n" represents the number of carbon atoms in one or more aromatic molecules. Further, the subscript "+" or "-" can be used in one or more abbreviated hydrocarbon notation, such as C ₃₊ or C _{3 -} , containing one or more abbreviated hydrocarbons. By way of example, the abbreviation "C ₃₊ " means one or more hydrocarbon molecules of three or more carbon atoms.

As used herein, the term "zone" may refer to an area containing one or more device items and / or one or more sub-zones. The device items may include, but are not limited to, one or more reactors or reactor vessels, a separation vessel, a distillation tower, a heater, an exchanger, a pipe, a pump, a compressor, and a controller. In addition, a device item, such as a reactor, dryer, or vessel, may further include one or more zones or sub-zones.

As used herein, the term "ratio of silica to alumina" may refer to the molar ratio of silicon oxide (SiO ₂ ) and aluminum oxide (Al ₂ O ₃ ) in the zeolite framework.

details

The following description is not intended to be taken in a limiting sense, but merely to illustrate the general principles of the exemplary aspects. The scope of the disclosure is determined with reference to the claims.

Applicants' invention involves a purification process using a solid adsorbent. With respect to the solid adsorbent, one necessary component may be a low reactive binder. The binder can be a high surface area, porous material, and can provide a bonding matrix. The binder may be selected from the group consisting of alumina, silica, clay, alumina silicate, titania, zirconia, and mixtures thereof. In one embodiment, the low reactive binder may be activated alumina. In another embodiment, the low reactive binder may be clay. The activated alumina generally contains alumina having a surface area in excess of 100 m ² / g and typically in the range of 100-400 m ² / g. Further, the activated alumina powder is preferably obtained by rapid dehydration of aluminum hydroxide, such as alumina trihydrate, in a stream of solid heat carrier or hot gas. Dewatering can be achieved in any suitable equipment using a stream of solid heat carrier or hot gas. Generally, the heating or contact time of the hot gas is very short term, usually from several seconds to 4 or 5 seconds. Normally, the temperature of the gas varies between 400 ° C and 1000 ° C. The process is generally referred to as flash calcination, for example as disclosed in U.S. Patent No. 2,915,365, which is incorporated herein by reference. However, other methods of calcination can be used.

Activated alumina suitable for use in the present invention has a median particle size in the range of 0.1-300 microns, preferably 1-100 microns, typically 1-20 microns. In certain instances, it is desirable to use alumina with a median particle size of 1-10 microns. The alumina can be pulverized to a desired particle size before and after activation. The activated alumina typically has a LOI (ignition loss) in the range of 5-12% at a temperature of 200 ° C to 1000 ° C. One source of activated alumina is gibbsite, a form of alumina hydrate derived from bauxite using the Bayer process. However, alpha alumina monohydrate, pseudoboehmite or alumina trihydrate can be used when sufficiently calcined. Other sources of alumina including clays and alumina alkoxides may also be used.

The clay suitable for use in the present invention may comprise a high purity clay having a small particle size. The bonding properties of the clay are well known in the art. Typically, the clay is naturally occurring, finely grained minerals such as kaolinite, halloysite, ilite and montmorillonite. Other clay groups include smectite, sepiolite, attapulgite, chlorite and the like. As a composition, the clay is a sheet-like aluminosilicate. The application of the binder is highly dependent on its purity and binding properties. The low reactivity of the binder is an important characteristic for the purposes of the present invention. The clay binder should not act as a catalyst in connection with all components of the hydrocarbon feed.

Another essential component of the present invention is zeolite. Zeolite is a crystalline aluminosilicate composition having a three-dimensional oxide framework formed from corners that are microporous and share AlO ₂ and SiO ₂ tetrahedra. The zeolite has a pore opening of uniform dimensions, has a considerable ion exchange capacity and is capable of reversibly desorbing the adsorbed phase dispersed throughout the inner void of the crystal without significantly displacing any atoms making up the permanent zeolite crystal structure . The zeolites that can be used in the present invention have pore openings of 5-10 Å.

Generally, the zeolite has the composition indicated by the following empirical formula:

M _{2 / n} O: Al ₂ O ₃ : bSiO ₂

Wherein M is a cation having a valence of "n" and "b" has a value of 2-500. A preferred zeolite is from 2: 1 to 6: and having a SiO ₂ / Al ₂ O ₃ ratio of the first and / or having a zeolite X, spores site, zeolite Y, zeolite A, mordenite, beta, and ferrierite crystal structure will be. Particularly preferred zeolites are zeolites X, Y and A.

The preparation of such zeolites involves the formation of a reaction mixture well known in the art and composed of a reactive source of components, which is then hydrothermally reacted to form a zeolite. Specifically, the synthesis of zeolite Y is described in U.S. Patent Nos. 3,130,007 and 4,503,023 and the synthesis of zeolite X is described in U.S. Patent Nos. 2,883,244 and 3,862,900, the disclosures of which are incorporated herein by reference.

Although the synthesis of zeolites, particularly zeolites X and Y, is well known, a brief description is provided herein for completeness. The reactive source of M includes, but is not limited to, halide and hydroxide compounds of alkali or alkaline earth metals such as sodium chloride, sodium hydroxide, potassium hydroxide, and the like. Aluminum sources include, but are not limited to, boehmite alumina, gamma alumina, and soluble aluminates such as sodium aluminate or tetraethylammonium aluminate. Finally, the silicon source includes, but is not limited to, silica, silica hydrosol, silicic acid, and the like.

The reactive source is combined with the reaction mixture having the composition in terms of the mole ratio of the oxides and the mixture then reacts to form a zeolite:

SiO ₂ / Al ₂ O ₃ = 8 to 12

M ₂ O / Al ₂ O ₃ = 2.5 to 4

H ₂ O / M ₂ O = 120 to 180.

As synthesized, the zeolite contains an "M" metal in the channels and / or pores. The function of these metal cations is to balance the negative charge of the zeolite lattice. Since these cations are not part of the framework, they are exchangeable and occupy the exchange site. The total amount of metal cations present in the zeolite is referred to as the stoichiometric amount or maximum ion exchange capacity of the zeolite. This amount is usually expressed as mol.

Since the initially presented metal cation in the zeolite is exchangeable, it can be exchanged for another (different) alkali metal, alkaline earth metal, hydrogen ion, ammonium ion or mixtures thereof. If the zeolite to be used contains some or all of the hydrogen or ammonium ions, such ions must be completely exchanged with alkali metals, alkaline earth metals or mixtures thereof before or during the preparation of the composite adsorbent.

Another required component of the shaped adsorbent of the present invention is a metal component (M _add ) selected from the group consisting of alkali, alkaline earth metals and mixtures thereof. This metal component (M _add ) is other than the metal cation (M) present at the exchange site of the zeolite. That is, M _add is presented in excess of and above the amount of exchangeable M metal ions present at the exchange site of the zeolite. Additionally, the M _add metal may be the same as or different from the M metal. For example, M metal in the zeolite can be potassium, but M _add can be sodium.

Specific examples of M _add include, but are not limited to, sodium, potassium, lithium, rubidium, cesium, calcium, strontium, magnesium, barium, zinc and copper. (Metal precursor) may be any compound that is decomposed to metal oxides (see below) under the activated conditions. Examples of such sources are nitrates, hydroxides, carboxylates, carbonates and oxides of metals. The shaped adsorbent does not necessarily achieve the same result, but it can be produced by combining the three components in any order and forming them into shaped articles.

In one method, an aqueous solution of alumina, zeolite and the desired metal compound is mixed and formed into a shaped article. For example, gamma alumina, zeolite X, and sodium acetate solutions may be combined in a dough followed by pellets, pills, tablets or spheres by means well known in the art (e.g., by oil titration) Or may be extruded or formed into a shape. A preferred method of forming a substantially round shape or body involves the use of a pan nodulizer. This technique utilizes a rotary fan or fan module to form a substantially round article or body by feeding an alumina component, a zeolite component, and a metal component solution onto a rotating fan or fan module.

Another method of forming molded articles is to mix powders of alumina, zeolite, clay and metal compounds and then form pellets, pills, and the like. A third method is to blend alumina and a zeolite component (powder), form it into a shaped article, and impregnate the shaped article into an aqueous solution of the metal compound. The forming step is performed by any of the means listed above.

When the molded article is obtained, it is cured or dried from ambient temperature to 200 ° C for a period of time of 5 minutes to 25 hours. The shaped article may be cured in a batch, such as a barrel or tray, or in a continuous process using a moving belt. Once the molded article is cured, it is activated by heating the cured article at a temperature of 275 DEG C to 600 DEG C for a period of 5 to 70 minutes. Heating may be performed on the article in a moving belt or moving fan where the article is directly fired to provide a finished solid adsorbent.

The finished adsorbent can now be used to remove contaminants from various hydrocarbon streams. The stream that may be treated includes, but is not limited to, hydrocarbon streams, particularly those containing saturated and / or unsaturated hydrocarbons. The olefin stream, such as ethylene, propylene and butylene, may be treated specially with an instant adsorbent. Such a stream contains one or more of the following pollutants: chloride, HCl, H ₂ O, CO, O ₂ , CO ₂ , COS, H ₂ S, NH ₃ , AsH ₃ , PH ₃ , Hg, And other S-containing or O-containing organic compounds.

A first embodiment of the present invention is a process for removing contaminants from a hydrocarbon stream comprising the steps of reacting a hydrocarbon comprising olefins, paraffins, aromatics, naphthenes, having a boiling point of from 50 DEG C to 180 DEG C, Contacting the stream with an adsorbent under adsorption conditions to remove a portion of at least one chloride containing contaminant, wherein the adsorbent comprises a zeolite component and a metal component to produce a hydrocarbon product stream. Embodiments of the present invention are any one or any one of the preceding embodiments of the preceding embodiments in this paragraph through the first embodiment in this paragraph, wherein the zeolite is selected from the group consisting of zeolite X, zeolite Y, zeolite A, . Embodiments of the present invention are any one or any one of the preceding embodiments in the preceding paragraph in this paragraph through the first embodiment in this paragraph, wherein the zeolite is zeolite X.

Embodiments of the present invention are any one, any or all of the preceding embodiments of the preceding paragraph in the paragraph through the first embodiment, wherein the adsorbent has a ratio of silica to alumina of from 2.0 to 2.5, preferably 2.1 to be. Embodiments of the present invention are any one, any or all of the preceding embodiments of the preceding paragraph in the paragraph through the first embodiment in which the adsorption conditions are selected from the group consisting of a temperature of from 50 ° C to 150 ° C, . Embodiments of the present invention are any one or any one of the preceding embodiments in the preceding paragraph in the paragraph from the paragraph above to any one or all embodiments wherein the metal component is sodium, potassium, lithium, rubidium, cesium, ≪ / RTI > Embodiments of the present invention are any one, any or all of the preceding embodiments of the preceding embodiments in this paragraph through the first embodiment in this paragraph, wherein the metal component is sodium. Embodiments of the present invention are any one, any or all of the preceding embodiments of the preceding paragraph in the paragraph from the paragraph above, wherein the zeolite is present in an amount of from 30% to 95% by weight of the adsorbent . Embodiments of the present invention are any one or any of the preceding embodiments in the preceding paragraphs in the paragraph through the first embodiment in this paragraph and wherein the step of transferring the hydrocarbon product stream to an extractive distillation unit for recovery of aromatics .

The adsorbent is for removing contaminants from the hydrocarbon stream comprising the zeolite component and the metal component. As the adsorbent, the zeolite is selected from the group consisting of zeolite X, zeolite Y, zeolite A and mixtures thereof. The adsorbent may have a silica to alumina ratio of 2.0-2.5. The metal component is an alkali metal selected from the group consisting of sodium, potassium, lithium, rubidium, cesium, and mixtures thereof. Preferably, the metal component is sodium. In addition, the zeolite is present in an amount of from 30% to 95% by weight of the adsorbent.

The hydrocarbon stream is purified by contacting the solid with the stream under adsorption conditions. Contact may be carried out in batch or in a continuous process and a continuous process is preferred. The adsorbent may be in the form of a stationary phase, a mobile phase or a spinning stream and is preferably a stationary phase. If a stationary phase is used, the feed stream can flow in an upflow or downflow direction, and an upflow is generally preferred for the liquid feed. If a mobile phase is used, the feed stream flow may be either cocurrent or counter current. Further, where a stationary phase is used, multiple beds may be used and disposed in one or more reactor vessels. The adsorption conditions include ambient temperature to 80 ° C, atmospheric pressure to 100 atm (1.01 x 10 ⁴ kPa), and contact time depending on whether the hydrocarbon stream is a liquid or gas stream. For liquid streams, the contact time, expressed in terms of LHSV, is between 0.5 and 10 hr ^-1 , while for gas streams the gas hourly space velocity varies between 500 and 10,000 hr ^-1 .

After a period of time, depending on the concentration of the contaminant, the size of the phase and the space velocity, the adsorbent is substantially consumed, i. E. Adsorbing the amount of contaminant (s) such that the level of contaminants in the purified stream exceeds an acceptable level. At this point, the adsorbent is removed and replaced with a fresh adsorbent. The spent adsorbent can be regenerated by means well known in the art and then repositioned for use. In a typical regeneration procedure, the adsorbent is first drained, depressurized and then cooled and purged with an inert stream. Subsequently, the heated hydrocarbons are removed from the phase in the downflow direction at 80 DEG C to 150 DEG C by warmed purging. Finally, the temperature is slowly raised from 280 DEG C to 320 DEG C and held there for at least 2 hours before cooling to ambient temperature.

The adsorbent can also be regenerated outside the adsorption bed. For example, the spent adsorbent can be transported offsite for regeneration. Typically, this procedure is performed by heating the inert and oxygen containing atmosphere in a specially designed oven.

Without further elaboration, it is believed that one skilled in the art can, using the preceding description, utilize the present invention to its fullest extent and practice various changes and modifications of the invention without departing from the spirit and scope of the invention, It is believed that the intrinsic characteristics of the < RTI ID = 0.0 > The preferred specific embodiments described above are therefore to be understood as exemplary only, and are not intended to limit the remainder of the disclosure in any way, but are intended to cover various modifications and equivalent arrangements included within the scope of the appended claims. In the above, all temperatures are listed in degrees Celsius, and all parts and percentages are by weight unless otherwise indicated.

A specific embodiment

While the following is described in conjunction with specific embodiments, it is to be understood that this description is intended to be illustrative, and not to limit the scope of the foregoing description and the appended claims.

A first embodiment of the present invention is a process for removing contaminants from a hydrocarbon stream comprising the steps of reacting a hydrocarbon comprising olefins, paraffins, aromatics, naphthenes, having a boiling point of from 50 DEG C to 180 DEG C, Contacting the stream with an adsorbent under adsorption conditions to remove a portion of the at least one chloride-containing contaminant, wherein the adsorbent comprises a zeolite component, a binder, and a metal component to produce a hydrocarbon product stream to be. Embodiments of the present invention are any one or any one of the preceding embodiments of the preceding embodiments in this paragraph through the first embodiment in this paragraph, wherein the zeolite is selected from the group consisting of zeolite X, zeolite Y, zeolite A, . Embodiments of the present invention are any one or any one or all of the preceding embodiments of the preceding paragraph in the paragraph through the first embodiment in which the binder is selected from the group consisting of alumina, silica, clay, alumina silicate, titania, zirconia, And mixtures thereof. Embodiments of the present invention are any one or any one of the preceding embodiments in the preceding paragraph in this paragraph through the first embodiment in this paragraph, wherein the zeolite is zeolite X. Embodiments of the present invention are any one, any or all of the preceding embodiments of the preceding paragraph in the paragraph through the first embodiment, wherein the adsorbent has a ratio of silica to alumina of from 2.0 to 2.5, preferably 2.1 to be. Embodiments of the present invention are any one, any or all of the preceding embodiments of the preceding paragraph in the paragraph through the first embodiment in which the adsorption conditions are selected from the group consisting of a temperature of from 50 ° C to 150 ° C, . Embodiments of the present invention are any one or any one of the preceding embodiments in the preceding paragraph in the paragraph from the paragraph above to any one or all embodiments wherein the metal component is sodium, potassium, lithium, rubidium, cesium, ≪ / RTI > Embodiments of the present invention are any one, any or all of the preceding embodiments of the preceding embodiments in this paragraph through the first embodiment in this paragraph, wherein the metal component is sodium. Embodiments of the present invention are any one, any or all of the preceding embodiments of the preceding embodiments in this paragraph through the first embodiment in this paragraph, wherein the zeolite is present in an amount from 30% to 95% by weight. Embodiments of the present invention are any one or any of the preceding embodiments in the preceding paragraphs in the paragraph through the first embodiment in this paragraph and wherein the step of transferring the hydrocarbon product stream to an extractive distillation unit for recovery of aromatics .

A second embodiment of the present invention is an adsorbent for removing contaminants from a hydrocarbon stream comprising a zeolite component, a binder component, and a metal component. Embodiments of the present invention are any one or any one of the preceding embodiments of the preceding embodiments in this paragraph through the first embodiment in this paragraph, wherein the zeolite is selected from the group consisting of zeolite X, zeolite Y, zeolite A, . Embodiments of the present invention are any one or any one of the preceding embodiments in the preceding paragraph in this paragraph through the first embodiment in this paragraph, wherein the zeolite is zeolite X. Embodiments of the present invention are any one or any one or all of the preceding embodiments of the preceding paragraph in the paragraph through the first embodiment in which the binder is selected from the group consisting of alumina, silica, clay, alumina silicate, titania, zirconia, And mixtures thereof. Embodiments of the present invention are any one, any or all of the preceding embodiments of the preceding paragraph in this paragraph through the first embodiment in which the adsorbent has a ratio of silica to alumina of 2.0-2.5. Embodiments of the present invention are any one or any one of the preceding embodiments in the preceding paragraph in the paragraph from the paragraph above to any one or all embodiments wherein the metal component is sodium, potassium, lithium, rubidium, cesium, ≪ / RTI > Embodiments of the present invention are any one, any or all of the preceding embodiments of the preceding embodiments in this paragraph through the first embodiment in this paragraph, wherein the metal component is sodium. Embodiments of the present invention are any one, any or all of the preceding embodiments of the preceding paragraph in the paragraph from the paragraph above, wherein the zeolite is present in an amount of from 30% to 95% by weight of the adsorbent .

Without further elaboration, it is believed that one skilled in the art can, using the preceding description, utilize the present invention to its fullest extent and practice various changes and modifications of the invention without departing from the spirit and scope of the invention, It is believed that the intrinsic characteristics of the < RTI ID = 0.0 > The preferred specific embodiments described above are therefore to be understood as exemplary only, and are not intended to limit the remainder of the disclosure in any way, but are intended to cover various modifications and equivalent arrangements included within the scope of the appended claims.

In the above, all temperatures are listed in degrees Celsius, and all parts and percentages are by weight unless otherwise indicated.

Claims (10)

A process for removing contaminants from a hydrocarbon stream comprising contacting a hydrocarbon stream comprising olefins, paraffins, aromatics, naphthenes and an adsorbent having a boiling point of 50 ° C to 180 ° C, preferably 50 ° C to 115 ° C, Wherein the adsorbent comprises a zeolite component, a binder and a metal component to produce a hydrocarbon product stream. The method of claim 1, wherein the zeolite is selected from the group consisting of zeolite X, zeolite Y, zeolite A, and mixtures thereof. The method of claim 1, wherein the binder is selected from the group consisting of alumina, silica, clay, alumina silicate, titania, zirconia, and mixtures thereof. 3. The method of claim 2, wherein the zeolite is zeolite X. The process of claim 1, wherein the adsorbent has a silica to alumina ratio of 2.0-2.5, preferably 2.1. The process of claim 1, wherein the adsorption conditions comprise a temperature of from 50 ° C to 150 ° C, preferably 120 ° C. An adsorbent for removing contaminants from a hydrocarbon stream, comprising a zeolite component, a binder component, and a metal component. The adsorbent according to claim 7, wherein the zeolite is selected from the group consisting of zeolite X, zeolite Y, zeolite A and mixtures thereof. The adsorbent according to claim 8, wherein the zeolite is zeolite X. 8. The adsorbent of claim 7, wherein the binder is selected from the group consisting of alumina, silica, clay, alumina silicate, titania, zirconia, and mixtures thereof.